Method of separating and purifying hydrogen



Nov. 25, 1935. Lis. TWOMEY l METHOD Of SEPARATING AND PURIFYING HYIIJROGEN Filed May 9, 1934 2 Sheets-Sheet l HUI WIWI' bbn/ LEE 5. TWOMEY M A, .van

Nov. 261, 1935.

Il ,'Jf FVW w v -f'fp L. s. Tw'oMEY 2,622,163

ME'IHQD OF SEPARATING AND PURIFYING HYDROGEN n Filed May 9, 1954 2 Sheets-S1166?. 2

LEE S. TWOMEY ENTR Patented Nov. 25, i935 pair The object' of my invention is to produce hydrogen of the last degree `of Ipurity 'fromivaterfgas or other gases in which hydrogen is present in material quantities.

The general method of operation hereinbelow described consists in first removing the carbon dioxide by solution or chemical combination, in then iiquefying and separating the greatest possible proportion of other impurities, in solidifying a further portion of the impurities, and in finally liquefying the hydrogen and separating the remainder of the impurities in solid form.

The invention may best be described in connection with the attached drawings which show in diagrammatic form an apparatus suitable for the application or the method steps or" the invention. It will be understood that Figs. l and 2 represent a unitary assemblage of apparatus, which may be viewed as a Whole by joining the right end of Fig. l to the left end of Fig. 2.

By Way oi illustration, the invention will be described in connection with the separation oi pure hydrogen from a semi-Water gas produced by the combustion oi coke with pure oxygen in the presence of steam, and having the follow-- ing analysis:

Hydrogen 40.0 Carbon monoxide 32.0 Carbon dioxide 25.0

Methane Oxygen Nitrogen The same description would apply to the separa tion of hydrogen from any Water gas.

In order to somewhat simplify the description the apparatus shown in the drawing is divided into` the following units: A is a quadruple refrigerant producing unit; B is the rst stage com pression unit for gas to be fractionated; C is a scrubbing unit for removing carbon dioxide; D is an apparatus for removing the las.t. .traces oi oxygen from the gas; E is the secoli" stage gas compression unit; F is a dehydrating interchanger; G is the main interchanger; H is a nitrogen cooled condenser for'methane carbon monoxide and nitrogen; I is a separator forre-l moval of these impurities both by liquefaction and by freezing. and J is-a combined hydrogen liquefier and a separator of these impurities by Unit A is substantially the apparatus for pro-Y ducing liquid reirigerants described and claimed in my copending application entitled Method of producing low temperature refrigeration", Serial It consists of four compressors IS, H, l2, and I3, adapted to the compression oi ammonia, ethylene, methane, andnitrogen respectively; four water cooled interchangers i4, i5,

stares rarest risica METHOD or sEPAas'rrNG AND PUarFYrNG nrnaoonn Lee S. Twomey, Vista, Calif.

Application May9, 1934, Serial No. '724,695

(Cl. Gil-175.5)

i6, and il' in which the compressed gases are dei `pril/cd of `their vheat oicompression and `brought back to substantially atmospheric temperature; four storage vessels i8, i9, 2i), and 2l in which liquid ammonia, liquid ethylene, liquid methane, 5 and liquid nitrogen are stored at pressures approximating 1l() pounds, 250 pounds, 295 pounds, and 220 pounds gauge respectively and .at ternperatures approximating 293 K., 240 K., 168 and 112 K. respectively; and three condensers 10 22, 23, and 2li in which ethylene, methane, and nitrogen are cooled to the above temperatures and thereby condensed by the evaporation of liquid ammonia, ethylene, and methane respectively.

These four refrigerants are used in later stages of the process and while I find it highly economical and preferable to produce them in the inanner above described and described at more length in the oopending application, it is permissible to 2g produce each of the refrigerants in any other manner.

Unit B comprises a compressor and a .water cooled nterchanger 3| The raw gas enters the i system from a source not shown through pipe 32 25 controlled by valve 33 and is compressed to a moderately high pressure, as for example 3i atm.

- absolute. At this pressure it is passed through interchanger 3| where it is brought back to atmospheric temperature and is then passed 30 through pipe 34 to scrubbing unit C.

Unit C consists of two vertical shells 35 and 35 provided with baiiles or trays 3l' and with rose nozzles or other spraying means 38 and 39. Nozzle 38 is supplied with water from a. source not 35 shown through pipe d and this Water, after counteriiow contact with the gas passing upwardly through the shell, is Withdrawn through pipe il controlled by valve d2. vThe gas, which is freed from the greater part oi its carbon dioxide con- 40 tact by solution in the Water, passes through pipe 43 to the lower part of shell 31, in which a pool 4d of a caustic alkali solution is maintained. A stream of solution is continuously drawn from this pool by a pump l5 and directed through pipe l5 46 to nozzle 39, from which it passes in counterflow to the gas stream to pool 44. The gas, which is now substantially` deprived of carbon dioxide, passes through pipe 4l to unit D.

Unit D comprises a furnace 4B of brick or other 50 refractory material, supplied with fuel gas and air through pipes 9 and 55, and provided with a stack 5l for the escape of combustion products. Within this furnace is set a heating chamber 52 the Wall of which is of gastight and pressure 5-5 resisting heat conducting material. This chamber is extended downwardly and out of the fulnaoe 'tojoin the outer shell of .an nterchaneel' l provided with tubes Eil. Within the chamber iS placed a substantially tubular member consisbim joined to the top edge or the one next below by a ring of sheet metal. These cones are lled with copper in the form of iine wire, s havings or turnings, the purpose of the conical form being to prevent leakage of gas around the edges of the mass of finely divided copper' as this mass shrinks under continued heating.

As shown by the directional arrows, the gas from Athe scrubbing unit enters the lower end of interchanger 53, passes upwardly through tubes :i and around the tubular member 55, being heated to a desired temperature (about 450 C.) by contact with the walls of chamber 52. It then passes into the upper end of member 55 and downwardly through the masses of heated copper, which cause complete combustion with hydrogen of whatever oxygen the gas may contain, and passes through a pipe 5S to the upper end of the space surrounding the tubes of interchanger 53, and flowing downwardly through this space is cooled in heating the upfiowing gas within the tubes, finally passing at substantially atmospheric temperature and under approximately 34 atm. pressure to unit E through pipe 57. A drain 58 having a valve 5g is provided for removing water which condenses in this interchanger.

Unit E comprises a compressor E6, which for economy of power is preferable multistage, and a water cooled interchanger 6i. The gas entering the compressor through pipe 5'.' is raised to a rela-tively high pressure, as for example 245 atm. absolute. At this pressure it is passed through Vmtercl'ianger Si where it is brought baci; to atmospheric temperature and is then passed through pipe S2 to the dehydrating interchanger F.

The dehydrating interchanger F is provided with a multiplicity of tubes $3 which are divided into groups by means of partitions 64 across the end tube chambers, and through these tube groups are individually conveyed various gases returning from later steps on the operation, as will be de- Hscribed. The space around the tubes is a conimon chamber which may be provided with the baffles indicated at 65 and with drain valves 66 for withdrawing condensed water from the pockets so formed. The temperature of this interchanger is so controlied that the gas leaving Vshell 6l' and passing through pipe 68 to unit G is substantially deprived of water. As this water is partly separated in the liquid form and partly as ice which accumulates in the interchanger, it is desirable to provide this unit in duplicate.

The main intel-changer G has a. shell 69 of the stepped construction shown and is provided with annular tube chambers 'I5- l0 arranged to divide the tubes Ii-'H into groups of different lengths. The interior of the shell is a common chamber through which all the tubes pass, but is preferably provided with baiiles l2 by which the gas flowing through the shell is repeatedly contacted with the tubes at an obtuse angle and under conditions of extreme turbulence. By this means the 'temperature within all the tubes at any one level is equalizedand. a very great temperature difference between the two ends of the interchangeris made possible.

The outermost tube chamber 'lilav is supplied with liquid anhydrous ammonia withdraym from .storage vessel i8 through pipe 73a. An expansion valve lia reduces the pressure on the anrmonia to substantially atmospheric, the arnr monia Vaporizing at the valve and in the tubes 'at its atmosphere pressure boiling point or about 240 K. Passing upwardly through the tubes, the ammonia flows through pipe 75a to a tube group of interchanger F, leaves these tubes at substantially atmospheric temperature and pressure, and returns through pipe 'i'a to the suction of ammonia compressor lil for recompression and condensation.

The next lower tube chamber '15b is supplied with liquid ethylene withdrawn from storage vessel 'lil through pipe 73h. An expansion valve 7Gb reduces the pressure on the ethylene to substantially atmospheric, whereupon it vaporizes as above described at a temperature about 168 K., flows through pipe Elib to and through intochanger F, and passes through pipe '15b at substantially atmospheric temperature and pressure to the suction of ethylene compressor l i.

The next lower tube chamber lilo is supplied with liquid methane withdrawn from storage vessel 29 through pipe An expansion valve 'Hc reduces the pressure on the methane to substantially atmospheric, whereupon it vaporizes as above described at a temperature about 112o K., flows through pipe 15e to and through interchanger F and passes through pipe itc at substantially atmospheric temperature and pressure to the suction of methane compressor i2.

The remaining tube chambers and their corresponding tube groups are supplied with cold gases returning from later steps in the operation, as will be described.

While a high degree of power economy is attainable by the storage refrigeration above described, it should be understood that the saine nal result as to purity may be attained and the apparatus simplified by omitting the three tube groups supplied with ammonia, ethylene, and methane respectively, together with the correspending passes through dehydrating interchanger F, and correspondingly increasing the supply or" liquid nitrogen to interchanger H.

If step refrigeration is used, the temperature of the cold end of the dehydrating interchanger F may be controlled by use oi the highest boiling refrigerant used in main interchanger G. The effectiveness of dehydrating interchanger F in reducing the amount of water vapor in the gas leaving it may be increased by the omission oi the ammonia step from main interchanger G, but this omission introduces the disadvantage of having 'lower temperatures with which to deal when periodically alternating the duplicate dehydrating interchanger. The question of the omission of the ammonia step or even the ethylene step is thus solely a matter of preference. The stream of gas, which has been consider'- ably lowered in temperature in passing through the main interchanger, passes throughipipe 'il to nitrogen refrigerator H which comprises a shell 78 provided with tubes i9. The'space around the tubes is supplied with liquid nitrogen withdrawn from storage vessel 2i through pipe i3d. An expansion valve ld reduces the pressure on the nitrogen to 3.5 atm., whereupon it vaporizes at a temperature about 99 K. in withdrawing heat from the partially puried hydrogen. The vaporized nitrogen through pipe Si changer G, thence through pipo 15d to and through interchanger F, and thence through pipe 16d to the suction of nitrogen compressor i3.

Unit I has a shell 82 of which the lower'portion acts as a storage vessel for a pool of condensate 83,

In the Lipper portion of the shell passes from condenser. H' to tube chamber' i3d of interplaced a tube bank 8G through which is passed cold hydrogen gas returning from unit J. The top of the shell is maintained by this tube bank at a temperature which should not be above 63 K. nor below 52 K., for reasons which will appear.

In condenser Il, methane, carbon monoxide, and nitrogen present in the gas stream are partially condensed out, the liquid condensate draining into pool 23 in unit I, and the lower portion of tube bank Si also produces some condensate which drains into the same pool. The liquid collected in this pool, which is a mixture of methane, carbon monoxide, and nitrogen in more or less the mme relative proportions as those in which they occur in the gas, is passed through an expansion valve 85 by which it is reduced to substantially atmospheric pressure, thence through pipe to tube chamber 70e of interchanger- G, thence through pipe Tte to and through interchanger F, and finally is discharged from the system through pipe 70e and open vaine li'f as a fuel gas at substantially atmospheric temperature and pressiue.

The upper portion of tube bank Sli in unit 1 is colder than `the lower portion and acts as a' freezer for methane, carbon monoxide, and nitrogen, the solids thus formed being largely collected as ice onthe tubes while a smaller portion (depending to some extent on gas velocity through apparatus) may be carried forward as snow into unit J.

Unit J comprises in its upper portion a shell 81, a plurality of tubes 88, and of bailles 89, the Whole forming an interchanger. The lower por- 'den of the shell provides storage space for a poo of liquid hydrogen 90.

The gas leaving unit I passes through pipe il! and an open valve S2 into the shell of unit J, Where it is cooled in countercurrent to the cold expanded hydrogen passing through the tubes. The space around the tubes is designed to aioid storage for considerable accumulations of snow, to minimize the frequency of shut-downs for thawing. The gas then passes through pipe 93 and a boiling coil Sli, immersed in hydrogen pool 9G, to an expansion valve S5 and an aspirator 05 by which, in cooperation, it is reduced from its initial pressure of 245 atm. to a pressure slightly in excess of atmospheric. Under the initial pressure the gas is liquefied in the boiling coil and by expansion is reduced in temperature to 20 K., being then introduced, mainly in the liquid condition, into hydrogen pool S0 which is in constant ebnllition at approximately 20.5?

The lower end of the shell is surrounded by a jacket 9'! which is constantly supplied with a small quantity of liquid hydrogen through pipe Sil and valve 29. This jacket is in communication with the suction side or" aspirator 96 through pipe 100 and the small pressure difference created by the aspirator slightly lowers the boiling point of the liquid hydrogen in the jacket, and the heat leaking into the jacket is consumed in boiling the jacket hydrogen and is thus prevented from reaching the lower end of pool 90, which it is deried to maintain in a quiescent state. A conical the upper. portion of pool 90 `passes upwardly through tubes Eil where it cools the gas lpassing downenrdly through the shellpthence through pipe H32 to tube bank B4 of unit I, thence through pipe |03 to tube chamber 'mf of interchanger G, thence through pipe 75j to and through interchanger F, and is finally withdrawn from the system through pipe '18j as hydrogen in the last degree of purity.

The objects of the above described manipulations ollowing the step of oxygen removal are: first, to liqueiy and to separate as a liquid the largest possible proportion of the impurities (methane, carbon monoxide, and nitrogen), separation in the liquid form being less troublesome and costly than the separation of solids; second, to attain the highest possible degree of purification by freezing and separating in the solid form the largest possible proportion of the impurities remaining after the liquid separation step.

The minimum*temperature at which these impurities may be removed in liquid form in the apparatus shown is limited by the temperature at which the mixture of impurities begins to solidify, as for reasonable operating convenience it is desirable to confine the accumulation of solids to certain specic vessels (units I and J) designed for the ready removal of ice. Therefore, in order to prevent the solidication of methane in unit H the outlet temperature of this unit is maintained at 90 K. or 2 above the freezing point of methane.

The temperature at the top of unit I may be varied within limits without greatly affecting the final result. This temperature should not be below about 52 K. as at lower temperatures the heat supplied to the' boiling coil will be insumcient to revaporize the liquid hydrogen. On the other hand it should not be higher than about 63Q as otherwise an excessive proportion of the total carbon monoxide and nitrogen will be carried over into unit J. The actual temperature realized in practice will depend on the proportioning of the areaof tube bank 84 to the total area of tubes 88.

The temperature of hydrogen pool 90 is self maintaining at that of boiling liquid hydrogen or about 20.5 K.

The effect of the above steps and temperatures is to produce a tail gas out of the Various units having the following proportions of impurities. In each of the columns except the rst, which states the percentage analysis of the original gas, the iigures represent the number of volumes of the stated impurity accompanying 100 volumes of pure hydrogen at the stage recited, up to the point Where the original quantity of hydrogen is reduced by combination with oxygen.

Original gas y 100.00 Volumes Hydrogen 40.0% Carbon dioxide 25.0% A62.50 do j Oxygen 0.3% 0.75 do Methane '0.6% 1.50 do Carbon monoxide 32.0% v 80.00 do Nitrogen 2.1% 5.25 do Total quantity 250.00 do l Purity of hydrogen 40.00%

After scrubbing in unit C Hydrogen 100.00 `Volumes Purity or hydrogen 53.33%

After removal of oazygen of unit D *Out of unit H at 90 .Ti-gos phase Hydrogen 98.500 Volumes Methane 0.042 do Carbon monoxide 1.002 do Nitrogen 1.445 do Total quantity 100.989 do Purity of hydrogen 97.528%

Out of unit I at 63 K. 52 K.

Hydrogen 98.50000 vol. Methane.. .00010 do. Carbon mono .00204 do. Nitrogen .00531 do.

Total quantity 98.57 do. 98.50745 do. Purity of hydrogen 99.925075 09.992%

Out of unit J at 20.5 K.

Hydrogen 98.50000 Volumes Carbon monoxide .00004 do Nitrogen .00008 do 'rotai quantity 98.50012 do Purity of hydrogen 99.999%

The figures above stated for methane at 63 at 20.5 are not represented to be accurate, being based on straight line projections of vapor pressure curves terminating at for methane, 52 for carbon monoxide and 57 for nitrogen. So far as I am aware, vapor pressure-determinations at lower temperatures have notbeen made public, and these'extremely small proportions of gaseous impurities are beyond the limits of accuracy of chemical analysis. The figures are, however, sunicently close to the truth to indicate an undeterminable but extremely minute proportion of impurity in hydrogen reduced to a temperature of 20.5 K. when provision is made for the physical separation of all substances liquefied or solidiiied at that temperature.

The structure of unit I is such that the gas is cooled from 90a down to the preferred outlet temperature in flowing over the tube bank Sil rather than by Contact with the wall of the shell. Part of the impurities frozen out by temperature reduction in this stage passes forward to unit J in the form of snow suspended in the gas stream', but the portion which remains behind in unit I is in the form of ice or frost of the tubes themselves instead of on the shell wall, a fact which greatly aids the rapidity' with which the `ice accumulation. may be removed by thawing.

tities of liquid hydrogen through pipe 104 and valve 105. The hydrostatic head of the liquid hydrogen materially retards the evolution of contaminating' vapors from the crystals.

As will be evident from the gures given above, the major portion (over 97%) of the impurities remaining in the gaseous form at 90 K. are

frozen even at 63 K. and the ice thus formed collects mainly in unit I, which will therefore require thawing at intervals varying with the ice storage capacity of this unit. The thawing may 'F be accomplished by closing Valves 92 and 85 and partially opening a valve |05 in pipe lill, this pipe connecting with pipe and in turn with pipes '15e and e, through the latter of which the liquefied impurities condensing in unit I are normally discharged. For the purpose of setting up a thawing cycle, pipe '16e is provided with a valve T03' and abranch i539 with a Valve H0. While operating, valve 103 is open and valve H0 closed, but when thawing this order is reversed, admitting the thawing gas to the suction of compressor 30 by which it is delivered through the series of units from C to I inclusive. Valve 33 in raw gas inlet pipe S2 should be closed while thawing, and also valve 'Md by which the nitrogen supply is withdrawn from unit H and the cycled gas allowed to warm up until the tube bank is completely defrosted.

When this step is completed, Valve 'Nid is opened to restore nitrogen refrigeration and circulation is continued until the temperature of the gas passing through pipe 80 is again reduced to K., at which time the other valve changes above described are reversed and the apparatus thereby put back on production.

I claim as my invention:

1. The method ofl separating and purifying g hydrogen from a gaseous mixture Vconsisting of hydrogen and gaseous impurities of higher boiling point which comprises: compressing a stream of said gaseous mixture to approximately 245 atm. absolute; cooling said stream to a temperature of substantial dehydration; further cooling said stream to approximately 90 l. and condensing a portion of the impurities; further cooling said stream to a temperature not substantially above 63 K. and thereby forming a further quantity of condensate and freezing a portion of said impurities; further cooling said stream under pressure to substantially 30 K. whereby the hydrogen is liqueed and substantially all remaining impurities are solidied as crystals; releasing the presssure on said hydrogen and thereby reducing its temperature to substantially 20 K.; collecting a body of said liquid hydrogen; maintaining the lower part of said body in a state of quiescence; maintaining ing said stream to a temperature of condensation of portion of thcirnpmities; further cooling said F' stream to a temperature at which further quantities of said impurities are condensed and a portion of said impurities are frozen; removing both said condensates; further cooling said stream removing both said condensates; g

under pressure to a temperature at which the hy- 75 drogen is liquefied and substantially all remaining impurities are solidified as crystals; reducing the pressure on said hydrogen and thereby reducing its temperature to the boiling point of hydrogen at said reduced pressure; collecting a body of said lioueiied hydrogen; maintaining the lower part of said body in a of quiesccnce; maintaining the upper part of said body in a state of ebullition, and withdrawing substantially pure gaseous hydrogen from above said body.

3. The method of removing a gaseous impurity from substantially water-free hydrogen which comprises: cooling a stream o said hydrogen to a temperature not above the freezing point of said impurity; retarding the flow o said stream to permit the deposition oi solid particles of said impurity, and withdrawing said stream from said deposited particles.

4. The method of removing impurities from a stream o' hydrogen which comprises: liquefying said hydrogen and freezing said impurities; collecting said liquefied hydrogen in a pool and sedimenting solidified particles into the lower part of said pool, and evaporating purified hydrogen from the upper part of said pool.

5. A method substantially and for the purpose set forth in claim 4, including the step of maintaining the lower part o said pool in a state of relative qui-essence by evaporating a relatively small proportion of liquid hydrogen withdrawn from said pool in heat interchange relationship with said lower part of said pool.

6. The method or removing impurities from a stream of hydrogen which comprises: liqueiying said hydrogen; forming soli-:i particles of frozen impurities within hydrogen stream, and separating said solid particles from said hydrogen by evaporating said hydrogen witliin an enclosure of space in which said solid particles are retained.

7. The method of removing a gaseous impurity from substantially water-free hydrogen which comprises: cooling a stream of said hydrogen to a temperature at which a portion of said impurity is frozen and retarding the iiow of said stream to permit the deposition of solid particles of said impurity; withdrawing said stream from said deposited solid particles; licpdefyinfr said hydrogen at a reduced temperature and thereby producing further solid particles of said impurity withinl said liquefied hydrogen.

8. In an operation in which a residue of hydrogen is separated from a stream of mixed gases containing higher boiling impurities by compression and cooling of said stream, the steps comprising: cooling said stream under pressure from substantially atmospheric temperature in six stages, to-wit: in the first and warmest stage, by heat interchange with expanded and evaporating liquid anhydrous ammonia; in the second stage by heat interchange with expanded and evaporating liquid ethylene; in the third stage by heat interchange with expanded and .evaporating .liquid methane; in the fourth stage by heat interchange with an expanded and evaporating condensate of impurities formed and separated in succeedingy stages: in fifthpstage oy heat interchange with expanded and cvsporating liquid nitrogen, and in the sixth and coldest stage by heat interchange with hydrogen cooled in the preceding stagesand further cooled by expansion; the gases produced by expansion and evaporation in each said stage being returned in heat exchange relation with said stream under pressure through all preceding stages.

9. Steps substantially as and for the purpose set forth in claim 8, in which streams of the gaseous ammonia, ethylene, methane, and nitrogen 5 produced by evaporation and expansion are separately compressed, cooled, and liquefied to provide the respective liquids for the first, second, third, and fifth cooling stages.

10. Steps substantially as and for the purpose set forth in claim 8, in which streams of the gaseous ammonia, ethylene, methane, and nitrogen produced by evaporation and expansion are heated to vsubstantially atmospheric temperature in eilecting a preliminary cooling of said mixed gas stream to a tempera-true of dehydration and are thereafter separately compressed, cooledandliqu'eed to provide vthe respective'liquids for the first, second, third, and fifth cooling stages. y

ll. The method of removing a gaseous impurity from substantially water-free hydrogen which comprises: cooling a stream of said hydrogen to ure at which a portion of said imezen and retarding the iiow of said stream to permit the deposition of solid particles of said impurit withdrawing said stream from said deposited solid particles; liquefying said hydrogen and entraining in said liquid any solid, particles of said impurity not previously deposited.

12. The method of effecting a partial separation of nitrogen and carbon monoxide from adniixture with hydrogen which comprises: liquefying streams of gaseous ammonia, ethylene, methane, and nitrogen by compression and-cooling; applying the expansion and evaporation of liquid streams of said ammonia, ethylene, and methane to the respctive nal cooling and liqueaction of said gaseous streams of ethylene, methane, and nitrogen; compressing a stream of said admixture and substantially removing carbon dioxide and water therefrom; reducing said mixture stream in a iii-st cooling eiiect to a ternperature at which carbon monoxide and nitrogen begin to condense; reducing said mixture in a second cooling effect to a lower temperature, thereby producing a condensate of nitrogen and carbon monoxide and a stream of purified hydrogen; separating said condensate from said stream; expanding said hydrogen stream to substantially atmospheric pressure; producing said rst cooling eiect by heat interchange between said mixture stream and a plurality of colder gas streams returned from later steps in the process 5 and also by heat interchange between said mixture stream and an expanded and evapozating stream of at least one of said liquid refrigerants; returning the gaseous methane so produced to be recompressed; producing said second cooling effect by heat interchange between said mixture stream and cooling media including said expanded hydrogen stream and an expanded and cvaporating stream of said liquid nitrogen; passing the hydrogen nitrogen discharged from '65 said second cooling effect in heat interchange relation with said mixture stream in first said cooling effect, whereby said hydrogen and nitrogen are brought to substantially atmospheric ternperature; withdrawing said expanded hydrogen stream, and returning last said nitrogen stream for recompression.

LEE S. TWOMEYL- 

